US5089242A - Method for selectively separating a non-ferrous metal - Google Patents
Method for selectively separating a non-ferrous metal Download PDFInfo
- Publication number
- US5089242A US5089242A US07/608,705 US60870590A US5089242A US 5089242 A US5089242 A US 5089242A US 60870590 A US60870590 A US 60870590A US 5089242 A US5089242 A US 5089242A
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- Prior art keywords
- precipitate
- solution
- precipitation
- blast furnace
- stage
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Classifications
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/02—Working-up flue dust
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S75/00—Specialized metallurgical processes, compositions for use therein, consolidated metal powder compositions, and loose metal particulate mixtures
- Y10S75/961—Treating flue dust to obtain metal other than by consolidation
Definitions
- the invention relates to a method for selectively removing Zn from an aqueous solution, for example a filtrate originating from a pressure leaching process for leaching Zn and/or Pb out of a powdered material, such as blast furnace dust, containing iron.
- a leaching process useful in the present method is known for example from EP-A-244910. That application describes how blast furnace dust is first separated by means of hydrocycloning into a low content Zn and Pb fraction which is suitable to be re-used in the blast furnace process, and a high content Zn and Pb fraction which undergoes further treatment.
- EP-A-244910 describes a process in which an aqueous slurry of blast furnace dust, comprising Zn, Pb and Fe is subjected to mechanical agitation, under an O 2 atmosphere under pressure and at elevated temperature.
- a HCl-containing reagent such as waste pickling liquor (FeCl 2 /HCl) is added and the pH adjusted to from 2.6 to 3.
- the mixture is then filtered while hot to remove a solid material containing Fe and leaving a filtrate rich in Zn and Pb.
- PbCl 2 crystallises out of the filtrate whilst the Zn-containing compounds remain in solution.
- the zinc is recovered from the remaining solution by treatment with sodium hydroxide, although no conditions of pH or temperature are recommended.
- the zinc content in such a precipitate may be up to approximately 30 wt %.
- the relatively Zn-rich fraction obtained in this way is not suitable for use as raw material for the zinc industry because high concentrations of Cl ions are present in the deposit. In this case, high concentrations of Cl are considered to be percentage weights of over 1%.
- a further drawback with the aforementioned process is that the Zn content of the deposit obtained in this way is still relatively low for re-use in the Zn industry. For optimum processing quality of the solid matter obtained, it is desirable for the Zn content to be approximately 70%.
- Zn may also be selectively removed from blast furnace dust by a leaching process which employs H 2 SO 4 .
- JP Kokai No 53-4705 describes a process in which H 2 SO 4 , H 2 O 2 and slaked lime are used to separately recover Zn and Fe.
- Fe(OH) 3 is precipitated at pH5 and Zn(OH) 2 at pH 7-8.
- JP Kokai No 52-82616 relates to a process for separating Fe, Zn, Pb and C in secondary blast furnace dust by treatment with H 2 SO 4 . In the final stage Zn(OH) 2 is recovered by the addition of slaked lime at pH 6.5 to 9.
- the present invention seeks to provide a process for selectively removing Zn from a filtrate originating from leaching using HCl-containing reagent, while giving Zn deposits having lower concentrations of Cl ions, compared to processes currently available.
- a method for selectively separating Zn from an aqueous solution containing ions of Zn and Fe which method comprises
- the present invention gives a method by which dust originating from blast furnaces may be fully processed into two main flows of re-useable solid raw materials, one for the blast furnace process itself, the other for the zinc and lead production industries.
- a particular advantage of the method in accordance with the invention is that the liquid remaining following the second precipitation stage can largely meet environmental control requirements directed at waste flows discharged directly into the sea.
- the present process is particularly suitable for treating liquids containing at least 10,000 ppm of chloride ions, obtained by leaching blast furnace dust using HCl.
- the method in accordance with the invention also has the advantage that in the first stage of the Zn precipitation, undesirable elements such as Si, Al and Fe are largely deposited out of the solution, and may, therefore, be removed. In the subsequent second stage of the precipitation, highly effective precipitation of essentially zinc may then take place. Furthermore, most of the Pb is removed from the solution in the second stage.
- the present inventors have discovered that efficient control of pH during the first stage of this precipitation is critical, as may be seen from FIGS. 1 and 2 of the accompanying drawings. If the pH is too low, that is just below 4, then too little of the undesirable elements will be deposited.
- the pH may be adjusted by addition of an alkali, such as an alkali metal hydroxide or an alkaline earth metal hydroxide, for example.
- Control of the pH during the second stage of the precipitation is not so critical.
- the pH may preferably be adjusted to a value of between 8 and 9.2 to obtain a precipitate having a reduced Cl ion concentration.
- precipitation in the first stage is carried out at a temperature of at least approximately 60° C. Under these conditions, the filtering quality of the slurry and the settling speed of the resultant precipitate are improved.
- the second precipitation stage is preferably carried out at a temperature of at least approximately 45° C. This results in an improved quality of precipitate in which there is less absorption of chlorine. This is thought to be due to the precipitate containing a reduced amount of zinc oxychloride in comparison to those obtained in the prior art. Naturally this improves the processing quality of the solid matter deposited as raw material for the zinc industry.
- FIGS. 3 and 4 of the accompanying drawings The effect of temperature and pH variation on the weight percent of chloride in the filter cake obtained in a one step precipitation process is indicated in FIGS. 3 and 4 of the accompanying drawings.
- FIG. 1 illustrates the degree of Zn lost from a solution when a series of precipitation processes were conducted, each at different pH.
- FIG. 2 illustrates the amount of Fe and Al remaining in solution after the firs precipitation step for a series of experiments each at different pH.
- FIG. 3 illustrates the degree of chloride ions contained in a filter cake when a series of precipitation processes were conducted each under different conditions of pH and temperature.
- FIG. 4 illustrates the degree of chloride ions contained in the filter cake for a series of precipitation processes conducted over a range of temperatures.
- Liquid originating from an autoclave pressure leaching process conducted on blast furnace dust using waste pickling liquor, and with a composition as given in Table 1 was treated by the currently known technique as well as by techniques in accordance with the invention.
- composition of Table 1 Using the currently known technique precipitation from the composition of Table 1 was performed in one stage by addition of sodium hydroxide up to a maximum pH value of 9.2.
- the composition of the solid matter obtained was as stated in Table 2 at various pH values.
- the Zn content in the solid matter was approximately 30% and the Cl content was approximately 15%, which is too high for the precipitate to be suitable as a raw material for the zinc industry.
- the same base liquid as given in Table 1 was treated in accordance with the invention with a precipitation process in two stages at 95° C. with intermediate removal of the deposited precipitate following the first stage.
- the component fractions following the first and second precipitation stage are given in Table 3.
- the precipitate obtained following the second precipitation stage was very rich in Zn, exceeding 70 % wt., while the Cl percentage was well below 1%, which gives a very good processing quality, suitable as a raw material for the zinc industry.
- the liquid treated in accordance with the invention also leaves a residual liquid the composition of which is as given in Table 4. From an environmental point of view, all these compositions of residual liquids are sufficiently low for enabling these liquids to be discharged into the sea without prior further treatment.
- FIG. 1 shows that the amount of Zn lost in the first precipitation stage is unsatisfactory when the pH is above 4.3, and particularly poor above pH 4.6.
- FIG. 2 shows that at below pH 4.0, the amount of Fe and Al removed by the first precipitation is unsatisfactory. Improved results were obtained at pH 4 and above.
Abstract
A method for selectively separating Zn from an acidic aqueous solution containing ions of Zn and Fe obtained by leaching of blast furnace dust using hydrochloric acid comprises first precipitating Fe from the solution and then treating the resultent Zn-containing solution with an alkali to precipitate Zn.
The Zn-containing solution is treated in two stages; in the first precipitation step the pH is adjusted to from 4.0 to 4.3.
Description
1. Field of the Invention
The invention relates to a method for selectively removing Zn from an aqueous solution, for example a filtrate originating from a pressure leaching process for leaching Zn and/or Pb out of a powdered material, such as blast furnace dust, containing iron.
2. Description of the Prior Art
A leaching process useful in the present method is known for example from EP-A-244910. That application describes how blast furnace dust is first separated by means of hydrocycloning into a low content Zn and Pb fraction which is suitable to be re-used in the blast furnace process, and a high content Zn and Pb fraction which undergoes further treatment.
More specifically, EP-A-244910 describes a process in which an aqueous slurry of blast furnace dust, comprising Zn, Pb and Fe is subjected to mechanical agitation, under an O2 atmosphere under pressure and at elevated temperature. A HCl-containing reagent such as waste pickling liquor (FeCl2 /HCl) is added and the pH adjusted to from 2.6 to 3. The mixture is then filtered while hot to remove a solid material containing Fe and leaving a filtrate rich in Zn and Pb. On cooling, PbCl2 crystallises out of the filtrate whilst the Zn-containing compounds remain in solution.
The above document suggests that the zinc is recovered from the remaining solution by treatment with sodium hydroxide, although no conditions of pH or temperature are recommended. The zinc content in such a precipitate may be up to approximately 30 wt %. However, the relatively Zn-rich fraction obtained in this way is not suitable for use as raw material for the zinc industry because high concentrations of Cl ions are present in the deposit. In this case, high concentrations of Cl are considered to be percentage weights of over 1%.
A further drawback with the aforementioned process is that the Zn content of the deposit obtained in this way is still relatively low for re-use in the Zn industry. For optimum processing quality of the solid matter obtained, it is desirable for the Zn content to be approximately 70%.
Zn may also be selectively removed from blast furnace dust by a leaching process which employs H2 SO4. JP Kokai No 53-4705 describes a process in which H2 SO4, H2 O2 and slaked lime are used to separately recover Zn and Fe. Fe(OH)3 is precipitated at pH5 and Zn(OH)2 at pH 7-8. JP Kokai No 52-82616 relates to a process for separating Fe, Zn, Pb and C in secondary blast furnace dust by treatment with H2 SO4. In the final stage Zn(OH)2 is recovered by the addition of slaked lime at pH 6.5 to 9.
The problems associated with high chloride ion concentration in the final Zn precipitate clearly do not apply to these processes which employ H2 SO4 as a leaching agent.
However, as HCl-containing reagents, such as pickling liquor, are more readily available, the present invention seeks to provide a process for selectively removing Zn from a filtrate originating from leaching using HCl-containing reagent, while giving Zn deposits having lower concentrations of Cl ions, compared to processes currently available.
3. Summary of the Invention
According to the invention there is provided a method for selectively separating Zn from an aqueous solution containing ions of Zn and Fe which method comprises
(i) providing a solution containing ions of Zn and Fe obtained by leaching of blast furnace dust using hydrochloric acid,
(ii) adjusting the pH of the solution to from 4.0 to 4.3 to precipitate Fe and removing the precipitate,
(iii) adjusting the pH of the resultant solution with alkali to precipitate Zn.
Therefore, in conjunction with EP-A-244910, the present invention gives a method by which dust originating from blast furnaces may be fully processed into two main flows of re-useable solid raw materials, one for the blast furnace process itself, the other for the zinc and lead production industries.
A particular advantage of the method in accordance with the invention is that the liquid remaining following the second precipitation stage can largely meet environmental control requirements directed at waste flows discharged directly into the sea.
The present process is particularly suitable for treating liquids containing at least 10,000 ppm of chloride ions, obtained by leaching blast furnace dust using HCl.
The method in accordance with the invention also has the advantage that in the first stage of the Zn precipitation, undesirable elements such as Si, Al and Fe are largely deposited out of the solution, and may, therefore, be removed. In the subsequent second stage of the precipitation, highly effective precipitation of essentially zinc may then take place. Furthermore, most of the Pb is removed from the solution in the second stage. The present inventors have discovered that efficient control of pH during the first stage of this precipitation is critical, as may be seen from FIGS. 1 and 2 of the accompanying drawings. If the pH is too low, that is just below 4, then too little of the undesirable elements will be deposited. If on the other hand the pH is too high, that is just above 4.3, then besides the said undesirable elements precipitating, too much zinc will precipitate and moreover the precipitate will not be easy to filter. The pH may be adjusted by addition of an alkali, such as an alkali metal hydroxide or an alkaline earth metal hydroxide, for example.
Control of the pH during the second stage of the precipitation is not so critical. However, the pH may preferably be adjusted to a value of between 8 and 9.2 to obtain a precipitate having a reduced Cl ion concentration.
It is also desirable that precipitation in the first stage is carried out at a temperature of at least approximately 60° C. Under these conditions, the filtering quality of the slurry and the settling speed of the resultant precipitate are improved. In addition the second precipitation stage is preferably carried out at a temperature of at least approximately 45° C. This results in an improved quality of precipitate in which there is less absorption of chlorine. This is thought to be due to the precipitate containing a reduced amount of zinc oxychloride in comparison to those obtained in the prior art. Naturally this improves the processing quality of the solid matter deposited as raw material for the zinc industry.
The effect of temperature and pH variation on the weight percent of chloride in the filter cake obtained in a one step precipitation process is indicated in FIGS. 3 and 4 of the accompanying drawings.
The invention will now be illustrated by reference to the accompanying drawings, in which
FIG. 1 illustrates the degree of Zn lost from a solution when a series of precipitation processes were conducted, each at different pH.
FIG. 2 illustrates the amount of Fe and Al remaining in solution after the firs precipitation step for a series of experiments each at different pH.
FIG. 3 illustrates the degree of chloride ions contained in a filter cake when a series of precipitation processes were conducted each under different conditions of pH and temperature.
FIG. 4 illustrates the degree of chloride ions contained in the filter cake for a series of precipitation processes conducted over a range of temperatures.
Liquid originating from an autoclave pressure leaching process conducted on blast furnace dust using waste pickling liquor, and with a composition as given in Table 1 was treated by the currently known technique as well as by techniques in accordance with the invention.
Using the currently known technique precipitation from the composition of Table 1 was performed in one stage by addition of sodium hydroxide up to a maximum pH value of 9.2. The composition of the solid matter obtained was as stated in Table 2 at various pH values. The Zn content in the solid matter was approximately 30% and the Cl content was approximately 15%, which is too high for the precipitate to be suitable as a raw material for the zinc industry.
The same base liquid as given in Table 1 was treated in accordance with the invention with a precipitation process in two stages at 95° C. with intermediate removal of the deposited precipitate following the first stage. The component fractions following the first and second precipitation stage are given in Table 3. The precipitate obtained following the second precipitation stage was very rich in Zn, exceeding 70 % wt., while the Cl percentage was well below 1%, which gives a very good processing quality, suitable as a raw material for the zinc industry.
Besides the zinc-rich solid matter, the liquid treated in accordance with the invention also leaves a residual liquid the composition of which is as given in Table 4. From an environmental point of view, all these compositions of residual liquids are sufficiently low for enabling these liquids to be discharged into the sea without prior further treatment.
TABLE 1 ______________________________________ Component parts of liquid to be treated (ppm) Zn Fe Al Mg Ca Mn Si Cl Pb ______________________________________ 10900 998 1216 707 2825 267 236 25200 880 ______________________________________
TABLE 2
______________________________________
One-stage precipitation of zinc from the liquid of Table 1
% % % % % % % % wt.
pH Zn Fe Al Mg Ca Mn Si Cl (g)
______________________________________
4.73 22.9 8.5 10.9 1.0 1.1 0.3 2.4 14.3 8.3
5.56 28.3 3.1 3.8 1.1 2.0 0.3 0.8 18.4 24.0
5.99 27.0 2.3 2.9 0.8 1.6 0.3 0.6 17.0 33.6
7.20 37.6 2.6 3.8 1.3 1.4 0.7 0.1 13.7 30.1
9.20 27.4 2.2 2.8 1.6 2.8 0.6 0.6 16.3 33.0
______________________________________
TABLE 3
__________________________________________________________________________
Two-stage precipitation in accordance with the invention
pH % Zn
% Fe
% Al
% Mg
% Ca
% Mn
% Si
% Pb
% Cl
wt. (g)
__________________________________________________________________________
a 4.28
11.1
21.39
22.98
0.08
0.61
0.01
4.13
0.12
4.14
4.8
9.08
74.0
0.04
0.04
4.55
0.53
1.65
0.52
0.07
0.35
13.6
b 4.24
8.7 22.32
24.56
0.02
0.21
0.01
4.43
0.86
4.77
4.5
9.10
73.0
0.02
0.08
4.32
0.53
1.54
0.51
4.01
0.11
14.6
c 4.18
7.0 21.00
22.30
0.03
0.37
0.03
3.93
0.78
6.4 6.1
8.98
70.5
0.01
0.02
4.25
0.12
1.67
0.48
4.05
0.5 13.1
__________________________________________________________________________
TABLE 4
__________________________________________________________________________
Waste water composition following two-stage precipitation (ppm)
no
Zn Fe Al Mg Ca Mn Si Pb Cl vol. (ml)
__________________________________________________________________________
a 6500
0.005
0.30
320 1890
120 32 3 15650
1490
11
0.001
0.20
2.6 1020
0.00
0.01
0.3 10500
2120
b 7760
0.005
0.30
395 2240
146 34 426 15600
1485
12
0.001
0.10
1.4 1223
0.00
0.01
4.9 11190
1920
c 9010
0.005
0.30
519 2860
189 40 523 16540
1500
13
0.001
0.10
13.2
1497
0.00
0.01
0.8 12372
2000
__________________________________________________________________________
Various additional tests were conducted using the liquid described in Table 1. The results are illustrated in FIGS. 1 to 4.
As may be seen from FIG. 1, the amount of Zn lost in the first precipitation stage is unsatisfactory when the pH is above 4.3, and particularly poor above pH 4.6. In addition, FIG. 2 shows that at below pH 4.0, the amount of Fe and Al removed by the first precipitation is unsatisfactory. Improved results were obtained at pH 4 and above.
Claims (4)
1. A method for selectively separating Zn from an aqueous solution containing ions of Zn and Fe which method comprises
(i) providing a solution containing ions of Zn and Fe obtained by leaching of blast furnace dust using hydrochloric acid,
(ii) adjusting the pH of the solution to from 4.0 to 4.3 to precipitate Fe and removing the precipitate,
(iii) adjusting the pH of the resultant solution with alkali at a temperature of at least 45° C. to precipitate Zn.
2. A method according to claim 1 in which the solution in (i) has been obtained by leaching blast furnace dust with waste pickling liquor from a hydrochloric pickling process.
3. A method according to claim 1 in which the first precipitation step is carried out at at least 60° C.
4. A method according to claim 1 in which the pH of the solution is adjusted to from 8 to 9.2 to precipitate Zn.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL8902783A NL8902783A (en) | 1989-11-10 | 1989-11-10 | METHOD FOR SELECTIVELY SEPARATING A NON-FERRO METAL. |
| NL8902783 | 1989-11-10 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US5089242A true US5089242A (en) | 1992-02-18 |
Family
ID=19855600
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US07/608,705 Expired - Lifetime US5089242A (en) | 1989-11-10 | 1990-11-05 | Method for selectively separating a non-ferrous metal |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US5089242A (en) |
| EP (1) | EP0427341B1 (en) |
| CA (1) | CA2029623C (en) |
| DE (1) | DE69006183T2 (en) |
| NL (1) | NL8902783A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5709730A (en) * | 1995-01-23 | 1998-01-20 | Cashman; Joseph B. | Hydrometallurgical processing of flue dust |
| US6117408A (en) * | 1999-06-29 | 2000-09-12 | Tetra Technologies, Inc. | Method of producing zinc bromide |
| US6361753B1 (en) * | 1995-12-26 | 2002-03-26 | Joseph B. Cashman | Converting zinc chloride to zinc oxide during the hydrometallurgical processing of flue dust |
| US6843976B2 (en) * | 2001-02-27 | 2005-01-18 | Noranda Inc. | Reduction of zinc oxide from complex sulfide concentrates using chloride processing |
| CN106029921A (en) * | 2014-02-18 | 2016-10-12 | 保尔伍斯股份有限公司 | Process for reducing the amounts of zinc (Zn) and lead (Pb) in materials containing iron (Fe) |
Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5759551A (en) * | 1993-04-27 | 1998-06-02 | United Biomedical, Inc. | Immunogenic LHRH peptide constructs and synthetic universal immune stimulators for vaccines |
| FR2810678B1 (en) * | 2000-06-23 | 2003-06-27 | Patrice Jean Albert Stengel | PROCESS FOR RECYCLING SLUDGES FROM BLAST FURNACES |
| WO2006119611A1 (en) * | 2005-05-10 | 2006-11-16 | George Puvvada | A process for the treatment of electric and other furnace dusts and residues containing zinc oxides and zinc ferrites |
| JP5596539B2 (en) | 2007-05-21 | 2014-09-24 | オーバイト アルミナ インコーポレイテッド | Method for extracting aluminum and iron from aluminum ore |
| EP2686458A4 (en) | 2011-03-18 | 2015-04-15 | Orbite Aluminae Inc | Processes for recovering rare earth elements from aluminum-bearing materials |
| EP2705169A4 (en) | 2011-05-04 | 2015-04-15 | Orbite Aluminae Inc | Processes for recovering rare earth elements from various ores |
| WO2012162817A1 (en) | 2011-06-03 | 2012-12-06 | Orbite Aluminae Inc. | Methods for preparing hematite |
| RU2014114938A (en) | 2011-09-16 | 2015-10-27 | Орбит Элюминэ Инк. | METHODS FOR PRODUCING ALUMINUM OXIDE AND VARIOUS OTHER PRODUCTS |
| CN104302791B (en) | 2012-01-10 | 2017-03-15 | 奥佰特氧化铝有限公司 | Method for processing red mud |
| RU2633579C9 (en) | 2012-03-29 | 2017-12-25 | Орбит Алюминэ Инк. | Methods of treating fly ash |
| WO2014008586A1 (en) | 2012-07-12 | 2014-01-16 | Orbite Aluminae Inc. | Processes for preparing titanium oxide and various other products |
| WO2014047728A1 (en) | 2012-09-26 | 2014-04-03 | Orbite Aluminae Inc. | Processes for preparing alumina and magnesium chloride by hc1 leaching of various materials |
| CN105189357A (en) | 2012-11-14 | 2015-12-23 | 奥佰特氧化铝有限公司 | Methods for purifying aluminium ions |
| WO2019122985A1 (en) * | 2017-12-22 | 2019-06-27 | Arcelormittal | Method for the treatment of iron-containing sludge |
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|---|---|---|---|---|
| US3164463A (en) * | 1961-10-10 | 1965-01-05 | Dravo Corp | Process for handling iron laden wastes in steel mills |
| US4018680A (en) * | 1976-02-24 | 1977-04-19 | Vol Roll A.G. | Process for separating iron, zinc and lead from flue dust and/or flue sludge |
| US4614543A (en) * | 1985-01-31 | 1986-09-30 | Amax Inc. | Mixed lixiviant for separate recovery of zinc and lead from iron-containing waste materials |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3375069A (en) * | 1965-07-23 | 1968-03-26 | Leonard A. Duval | Process for removing zinc oxide from iron oxide flue dust by the use of spent pickle liquor |
| FI58349C (en) * | 1978-04-04 | 1981-01-12 | Outokumpu Oy | FOERFARANDE FOER BEHANDLING AV METALLHALTIGA STOFT OCH AVFALL FRAON METALLURGISK INDUSTRI |
| FR2459293B1 (en) * | 1979-06-15 | 1985-09-27 | Siderurgie Fse Inst Rech | METHOD AND DEVICE FOR HYDROMETALLURGICAL TREATMENT OF METALLURGICAL DUST |
| NL8601147A (en) * | 1986-05-06 | 1987-12-01 | Hoogovens Groep Bv | SEPARATING NON-FERRO METALS FROM IRON-CONTAINING POWDER-MATERIAL. |
-
1989
- 1989-11-10 NL NL8902783A patent/NL8902783A/en not_active Application Discontinuation
-
1990
- 1990-11-05 US US07/608,705 patent/US5089242A/en not_active Expired - Lifetime
- 1990-11-06 EP EP19900202927 patent/EP0427341B1/en not_active Expired - Lifetime
- 1990-11-06 DE DE1990606183 patent/DE69006183T2/en not_active Expired - Fee Related
- 1990-11-09 CA CA 2029623 patent/CA2029623C/en not_active Expired - Fee Related
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|---|---|---|---|---|
| US3164463A (en) * | 1961-10-10 | 1965-01-05 | Dravo Corp | Process for handling iron laden wastes in steel mills |
| US4018680A (en) * | 1976-02-24 | 1977-04-19 | Vol Roll A.G. | Process for separating iron, zinc and lead from flue dust and/or flue sludge |
| US4614543A (en) * | 1985-01-31 | 1986-09-30 | Amax Inc. | Mixed lixiviant for separate recovery of zinc and lead from iron-containing waste materials |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5709730A (en) * | 1995-01-23 | 1998-01-20 | Cashman; Joseph B. | Hydrometallurgical processing of flue dust |
| US6428599B1 (en) | 1995-01-23 | 2002-08-06 | Joseph B. Cashman | Iron-rich residue recyclable from the hydrometallurgical processing of flue dust |
| US6361753B1 (en) * | 1995-12-26 | 2002-03-26 | Joseph B. Cashman | Converting zinc chloride to zinc oxide during the hydrometallurgical processing of flue dust |
| US6117408A (en) * | 1999-06-29 | 2000-09-12 | Tetra Technologies, Inc. | Method of producing zinc bromide |
| US6843976B2 (en) * | 2001-02-27 | 2005-01-18 | Noranda Inc. | Reduction of zinc oxide from complex sulfide concentrates using chloride processing |
| CN106029921A (en) * | 2014-02-18 | 2016-10-12 | 保尔伍斯股份有限公司 | Process for reducing the amounts of zinc (Zn) and lead (Pb) in materials containing iron (Fe) |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0427341A1 (en) | 1991-05-15 |
| DE69006183T2 (en) | 1994-08-04 |
| CA2029623C (en) | 1996-04-30 |
| CA2029623A1 (en) | 1991-05-11 |
| EP0427341B1 (en) | 1994-01-19 |
| NL8902783A (en) | 1991-06-03 |
| DE69006183D1 (en) | 1994-03-03 |
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